PUMPING OF CELLULOSE CONTAINING MIXTURES

Abstract: A method of conveying a relatively viscous, cellulose containing mixture, such as a premix comprising cellulose dispersed in a solution of amine oxide and water, with the use of a reciprocating piston pump, e.g. a so-called concrete pump.

Description: Pumping of Cellulose Containing Mixtures TECHNICAL FIELD This invention relates to a method of conveying a cellulose containing mixture having a paste or slurry like consistency. In particular, but not exclusively, the mixture comprises cellulose, amine oxide and water. The invention also relates to a system of conveying a cellulose containing liquid mixture. BACKGROUND ART Cellulose containing mixtures are well known in different fields of application. In the wood processing and paper making industries there is a need to convey fiber suspensions of pulp having a relatively high consistency (i.e. percentage by weight of dry cellulose material in solution). In other industries, such as the textile industry, there is the need to convey cellulose containing solution to a shaping station where the solution is adapted to be shaped and subsequently regenerated into a cellulosic product, such as a fiber or filament or cellulosic rod, tubing, plate or film. In the pulp and paper industry, it is often necessary to convey a fiber suspension between different places. When the consistency of the suspension is low, i.e. up to about 5%, there are few problems with the fiber suspension being able to flow freely. Problems occur, however, when the consistency of the fiber suspension is greater than about 5%. When the consistency is higher than about 5%, there is only a small amount of free liquid between the fibers and the fibers form a strong fiber network the strength of which depends mainly on the consistency of the suspension. The characteristics of medium or high consistency fiber suspensions are quite different from those of a true liquid and their handling becomes more difficult the higher the consistency. Conventionally in the pulp and paper industry, the conveyance of fiber suspensions has been performed with the use of rotary positive-displacement pumps. However, since conventional screw or gear pumps are heavy, large, expensive and break down relatively frequently, there has been a tendency in recent times to replace such rotary positive- displacements with centrifugal pumps, especially where the need is to convey liquid-fiber suspensions having a consistency in excess of 8%. US patents Nos. 4884943, 4981413, 5000658 and 5058615 disclose the use of centrifugal pumps for pumping relatively high consistency fiber suspensions. In pumping liquid-fiber suspensions having a consistency of greater than 8%, it has been proposed to feed the suspension to the suction opening of the centrifugal pump by means of a special screw feeder. However, with such pumps it has not been commercially possible to pump fiber suspensions having a consistency which approaches 15%. An alternative solution to pumping relatively high consistency fiber suspensions has involved diluting the pulp prior to the centrifugal pump and re-thickening the pulp after pumping. However this known technique adds to the complexity and cost of the pumping apparatus. In McCorsley US Patent No 4,416,698, the contents of which are incorporated herein by way of reference, there is described a method of producing cellulose filaments from a solution containing cellulose dissolved in a suitable solvent, for example a tertiary amine N-oxide and water. The water acts to swell the pulp fibers and assists in contacting the fibers with the tertiary amine oxide. At elevated temperatures and reduced pressure, the cellulosic material is dissolved in the tertiary amine oxide-water mixture to form a solution having a relatively high solids content. The cellulose dope so formed has to be retained at an elevated temperature to prevent it from solidifying. It is important to handle the cellulose dope carefully in subsequent transporting operations to avoid the breakdown in the homogeneity of the mixture. For example, if the dope is subjected to too severe a pumping operation, the tertiary amine N-oxide tends to separate or become "squeezed" out of the solution. Apart from the rotary, screw and gear pumps referred to above, another type of positive-displacement type is the reciprocating piston pump. Normally, reciprocating pumps are not well suited to pumping very dirty or very viscous liquids because of the possibility of "clogging" of the pump parts. However, US patents nos. 4178142 and 4373875 disclose a double-cylinder so-called "concrete pump" which is mainly intended for the conveyance of cement or concrete or other viscous material, e.g. settling mud. However, there is no suggestion in these patent specifications that such concrete pumps can be used for conveying cellulose containing mixtures, in particular cellulose dispersed in a suitable solvent such as tertiary amine oxide and water. The handling of such mixtures of cellulose, amine oxide and water is extremely difficult to achieve without breakdown occurring in the homogeneity of the mixture. DISCLOSURE OF THE INVENTION An object of the present invention is to provide a method of pumping a cellulose containing liquid mixture, e.g. a cellulose-amine oxide-water mixture, using a reciprocating piston pump, e.g. a so-called concrete pump such as a double cylinder reciprocating pump. According to one aspect of the present invention there is provided a method of conveying by means of pumping apparatus a mixture of cellulose and at least one liquid, the mixture has a cellulose of at least 8% by weight, wherein the pump is a reciprocating piston pump. Premixes comprising mixtures of cellulose, amine oxide and water, are particularly difficult to handle and convey without the cellulose breaking down or the amine oxide becoming separated from, or squeezed out of, the mixture. It has been found, however, that by using a reciprocating piston pump operating at relatively low reciprocating speeds, such premixes do not deteriorate in quality and the mixed components remain in a homogeneous state. The method is particularly suited to premixes having a consistency (proportion of dry weight of cellulose in the mixture) in excess of 8%, e.g. at least 10% or preferably at least 12%, such as 13%. The method can also be advantageously used for mixtures having consistencies in excess of 15%, e.g. up to 20%. The invention is particularly suited to conveying a premix at an elevated temperature, typically in excess of 150°F, e.g. 176°F, and comprising a mixture containing cellulose dispersed in a solvent for cellulose comprising amine oxide and water. Suitably such a mixture comprises approximately 13 parts by weight of cellulose and 87 parts by weight of amine oxide and water. Conveniently the mixture comprises 13% by weight of cellulose, 72% by weight of amine oxide and 15% by weight of water. Preferably the reciprocating pump is thermally lagged and may be heated, e.g. by means of a hot water jacket, to ensure that the mixture remains at an elevated temperature. Conveniently the solvent for cellulose comprises any suitable tertiary amine oxide which is compatible with water. Preferred tertiary amine oxides are cyclic mono (N- methylamine-N-oxide) compounds such as, for example, N- methyl-morpholine-N-oxide, N-methylpiperidine-N-oxide, N- methylpyrrolidone-oxide, dimethylcyclohexylamine oxide and the like. According to another aspect of the invention there is provided a system for preparing and conveying a cellulose containing liquid mixture comprising a premixer for mixing the constituents of the mixture, a storage hopper into which the mixture is stored and a reciprocating piston pump for conveying the mixture in the storage hopper to a further processing station. BRIEF DESCRIPTION OF THE DRAWINGS An embodiment of the invention will now be described, by way of example, with particular reference to the accompanying drawings, in which: Figure 1 is a schematic representation of apparatus for forming a mixture containing at least cellulose and a solvent for the cellulose; Figures 2a and 2b are schematic side and sectional views, respectively, showing particulate material being deposited on the outside of a filtering sleeve; Figures 3a and 3b are schematic side and sectional views, respectively, showing particulate material previously deposited on the outside of a filtering sleeve being removed therefrom; Figure 4 is a schematic sectional view, on an enlarged scale, of a premixer of the apparatus shown in Figure 1; Figure 5 is a part sectional view, on an enlarged scale, of a storage hopper of the apparatus shown in Figure 1, and Figures 6 and 7 are, respectively, a schematic end sectional view and view from above, on enlarged scales, of part of a reciprocating dual piston pump of the apparatus shown in Figure 1. BEST MODES OF CARRYING OUT THE INVENTION Figure 1 shows schematically apparatus, generally designated by the reference numeral 1, for forming a mixture of cellulosic material dispersed in a solvent for the cellulose. The apparatus 1 comprises a first set of pulp rolls 2, a second set of pulp rolls 3, a pulp shredding device 4 and associated fan 23, pulp separators 5a and 5b, filtering means 6, premixer 7a and 7b, storage hoppers 84 and 85 and reciprocating dual piston pumps 88 and 89. A multi-layered first web 9 of cellulosic material is formed by drawing webs from the first set of pulp rolls 2 using a lower pair of nip rolls 8 and an upper pair of nip rolls 10. In its path between the nip rolls 8 and 10, the first web 9 is fed between a pair of spaced apart web guide plates 11. A multi-layered second web 12 of cellulosic material is also formed by drawing webs from the second set of pulp rolls 3 using a lower pair of nip rolls 13 and an upper pair of nip rolls 14. The second web is guided between the nip rolls 13 and 14 by means of spaced apart guide plates 15. The guide plates 11 and 15 are positioned between the nip rolls 8 and 10 and 13 and 14, respectively, so as to guide the multi-layered webs 9 and 12 between the nip rolls without the need for operator interaction. Preferably the guide plates 11 and 15 are hinged for access in case during use there is a blockage between the guide plates. As can be seen in Figure 1, there are eight pulp rolls in the first set of pulp rolls 2 and four pulp rolls in the second set of pulp rolls 3. Pulp rolls are supplied to end users on the basis of the viscosity of a liquid product produced in a predetermined manner from the pulp material. Although viscosity ratings vary from batch to batch, an end user can select stock rolls having viscosity ratings from pre-selected viscosity bands. Since it has been found that a better quality of cellulosic premix is obtained by mixing together rolls having high and low viscosity ratings in order to produce a "mix" of pulp materials having a desired intermediate viscosity rating, the rolls in the first set of pulp rolls 2 have a viscosity rating in a lower value band and the rolls in the second set of pulp rolls 3 have a viscosity rating in a higher value band. The speed of travel of the webs 9 and 12 to the shredding device 4 is controlled to provide a mixture of pulp material having the desired viscosity rating. In order to produce a consistent premix, it is important to accurately control the amount of cellulose which is added to the premixers 7a and 7b for mixing. Since pulp rolls contain both cellulose and water, it is necessary to determine the water content of the pulp rolls and to derive the bone-dry weight of cellulose present. In the simplest form, shredded pulp from the shredding device 4 can be weighed in weighting apparatus (not shown) before the desired weight of pulp is added to the premix 7a or 7b. If this method is employed, it is assumed that the pulp rolls consist of a set percentage by weight of cellulose and a set percentage by weight of water, e.g. 94% by weight of cellulose and 6% by weight of water. Preferably, however, the bone-dry weight of pulp material is calculated as it is fed to the shredding device with the use of sensing means 16 and 17 sensing the webs 9 and 12, respectively. Each sensing means 16, 17 comprises a beta ray scanner for measuring the weight per unit area of the composite layered web 9 or 12 and optionally also comprises a moisture measuring device employing microwave absorption techniques to measure the moisture content of the web 9 or 12. If moisture measurement is not employed, the moisture content of each web is considered to be about 6% by weight of the web, the remaining 94% by weight being cellulose. With signals for the weight per unit area of each web 9, 12, the width of each web and the moisture content of each web, the amount of cellulose delivered to the shredding device 4 can be calculated and this figure used to control the amount of cellulose added to each premixer. Metal detectors 18 and 19 are also provided to detect for the undesirable presence of metal within the webs 9 and 12. If metal is detected the process can be automatically stopped. The multi-layered first and second webs 9 and 12 of cellulosic material are fed into the inlet of the shredding device 4 where the webs are cut or comminuted into irregular flakes or particles of pulp material. The shredding device 4 is provided with rotating cutter knives 20 which are designed to cut or tear the cellulosic web material with minimum compression of the cut edges of the web material. This is desirable so that the cut web material is later better able to expand and mix with amine oxide and water. A particular preferred typed of pulp shredder is the cutter manufactured by Ulster Engineering and marketed by Birkett Cutmaster Limited known as the "AZ 45 Special". Such a shredder is provided with a knife type cutter (type 31 mm x 7 hook) . The rotating knives 20 of the shredding device 4 rotate at approximately 140 rpm and cut the cellulosic material into irregular shapes or flakes up to about 1 to 20 cm 2 , typically from about 3 to 15 cm 2 . However, in addition to producing these relatively large flakes or particles of cellulosic material, the cutter knives also generate a quantity of much finer cellulosic particles or "pulp dust". Typically, during the web shredding process, up to 99% of the web material is cut into these larger flakes or particles of cellulosic material with the remaining 1% being formed into pulp dust. The cut and shredded pulp material, including the pulp dust, exits from the outlet of the shredding device 4 and is conveyed via circular section ducting 21 to a diverter valve 22. The pulp material is conveyed in an air stream created by the air fan 23 at the outlet of the shredding device 4 which sucks in air at air inlet A through a filter 24. This fan has vanes which are fitted with cutting blades and these help to shred and break up further the particles of cellulosic material exiting from the shredding device 4. The process operates as a batch process and, depending on which part of the batch process is in operation, the diverter valve 22 directs the cut pulp from ducting 21 either via ducting 25 to the pulp separator 5a or via ducting 26 to the pulp separator 5b. Each of the pulp separators 5a and 5b operates in a similar manner and only pulp separator 5a will be described in detail hereafter. The pulp separator 5a has an inlet 27, a first outlet 28 arranged in line with the first inlet 27 and a second outlet 29 offset from a path between the inlet 27 and first outlet 28. A mesh screen 30 is arranged at an angle between the direct path between the inlet 27 and first outlet 28. In use, the cut pulp material including the pulp dust is conveyed in a stream of air via the ducting 25 through the inlet 27 and is directed towards the first outlet 28. The mesh screen 30 has a mesh size of 0.1 inch (2.54mm) and allows the pulp dust, up to a particle size of 0.1 (2.54mm) inch and the conveying air stream to pass therethrough and out through the first outlet 28. The larger particles of cut cellulosic material which are too large to pass through the mesh of the screen 30, are deflected by the angled screen 30 downwardly through the second outlet 29. The pulp dust and conveying air stream which exits from the first outlet 28 is passed via ducting 31 and 32 to an inlet of the filtering means 6. The filtering means 6 serves to extract the pulp dust from the conveying air stream. A particularly suitable form of filtering means 6 comprises the JETLINE V filter manufactured by NEU Engineering Limited of Woking, Surrey, England. Such a filtering means 6 has a plurality of filter sleeves 40 (see Figures 2a, 2b, 3a, 3b) arranged vertically in rows, e.g. twelve rows of eight filter sleeves per row. Each filter sleeve 40 of just under 1 m 2 gives a total area for all 96 sleeves of 100m 2 square section conveniently comprising needle-felt sleeve which is supported on a rigid vertical frame 41 made of anti-corrosion steel wire. The filtering means 6 operates under positive pressure, the pulp dust laden inlet air being blown upwardly and radially inwardly through the tubular filter sleeve 40 in the direction of the arrows in Figure 2a. A "cake" 42 of pulp dust builds up on the outside of the sleeves 40 and "clean" air is conveyed upwardly through a venturi shaped outlet tube 44. Clean air exits at 45 (see Figure 1) in the direction of arrow B. The cakes 42 of pulp dust are removed from the filter sleeves 40 by pulsing air periodically downwardly through the integral venturi tube 44, with each row of filter tubes being cleaned in turn. Each cleaning process involves injecting compressed air downwardly via duct 46 from compressed air line 47 into each sleeve 40 via the venturi tube 44. This momentarily reverses the air flow through the filter sleeve and abruptly inflates the filter sleeve thus throwing off the cake of pulp dust (see Figure 3a and 3b). The pulp dust removed from the filter sleeves 40 drops into a storage hopper 50 at the bottom of the filtering means 6. The storage hopper 50 has four sides angled inwardly and downwardly towards a rotary valve 51. Each of the four walls of the hopper 50 are provided with a pair of blow nozzles 52 which are periodically operated to prevent the pulp dust accumulating on the angled side walls of the hopper 50. On rotation of the rotary valve 51 and on operation of the pulp dust fan 55, pulp dust is conveyed via ducting 56 to a diverter valve 57. Depending on which "batch" path is in operation, the diverter valve 57 either diverts the flow of pulp dust via ducting 58a to cyclone separator 59a or via duct 58b to cyclone separator 59b. Assuming the diverter valve 57 is set to divert the pulp dust and conveying air to the cyclone separator 59a, pulp dust exits from the latter and is conveyed via ducting 60 to T-into a duct 62 leading from the second outlet 29 of separator 5a. A rotary valve 61 is provided in ducting 60 and a further rotary valve 63 is provided in ducting 62 adjacent its inlet end. Provided these valves 61 and 63 are turning, the pulp dust conveyed via ducting 60 is re-combined with the larger particles of cut cellulosic material separated by the pulp separator 5a. Outlet air from the cyclone separator 59a is cycled back to the separating means 6 via ducting 70 in order to extract any further pulp dust which still might be present in the air exiting from the cyclone 59a. The separator 5b is brought into operation when the diverter valve 22 is set to divert the cut pulp and conveying air via ducting 26. Pulp dust exists from the first outlet of the separator 5b and is conveyed via ducting 72 and 32 to the filtering means 6. The diverter valve 57 ensures that pulp dust from the filtering means 6 is diverted via ducting 58b to the cyclone separator 59b from where pulp dust passes via outlet 74 for re-combination with coarser particles of cellulosic material separated in the separator 5b and exiting via ducting 75. This re¬ combination of pulp dust proceeds when rotary valves 76 and 77 are operational and not in their stationary condition. Approximately 1,0001b of wood pulp is processed in each batch and four batches are processed each hour. Thus of the 4,0001b of wood pulp processed each hour, approximately 1% (i.e. 401b) of pulp dust is re-combined with the larger particles of cut pulp material. Without the provision of the filtering means 6, this amount of wood pulp dust would have been lost to the process. The shredded pulp and pulp dust from the ducting 62 and 75 is fed to inlets 80 and 81, respectively, of the premixers 7a and 7b, respectively, depending on which batch is being processed. Each of the inlets 80 and 81 is conveniently heated by means of a hot water jacket 82 (see Figure 4) through which hot water, e.g. at 120°F (49°C) is circulated. The hot water is supplied via hot water supply pipe 82a and is returned via hot water return pipe 82b. Since the premixers 7a and 7b are substantially identical, only premixer 7a will be described in detail. The premixer 7a has four further inlets 83 (only one of which is shown) for the introduction therein of a water solution of tertiary amine oxide, the mixture consisting of 78% parts by weight of amine oxide and 22% parts by weight of water. A particularly preferred tertiary amine oxide is N-methyl-morpholine-N-oxide. The temperature of the amine oxide solution is carefully controlled to a desired temperature of approximately 180°F (82°C), e.g. 176°F (80°C), prior to its introduction into the premixer. The amount of amine oxide solution introduced into the premixer 7a is carefully controlled by a mass flow meter and a valve 83c in supply line 83d so as to produce a mixture with the added pulp consisting of approximately 13 parts by weight of cellulosic material and 87 parts by weight of amine oxide and water. Typically in each batch approximately 80001b of amine oxide solution and approximately 12001b of shredded pulp are added to the premixer. A stabiliser, such as powdered propyl gallate, is also conveniently added to each premixer for mixing with the other materials. The stabiliser is added to prevent or reduce the decomposition of the amine oxide and the decomposition of the cellulose. It is suitably added to the shredded pulp just prior to the latter being introduced into the premixer. Other additives may be added at this stage. Examples of such additives are dulling agents, e.g. titanium dioxide, viscosity modifiers and pigments. The premixer 7a comprises a mixing chamber within which is mounted a horizontal shaft 65 having radial paddles 65a extending therefrom. The paddles 65a are in the form of plough blade stirrers and extend radially conveniently in different axial planes. The horizontal shaft 65 is driven by an externally mounted motor and rotates relatively slowly at approximately 72 r.p.m.. Mounted in line in the walls of the mixing chamber of the premixer 7a are four spaced apart refiner mixers 67 (only one of which is shown in Figure 4) each driven by an externally mounted motor 67a to rotate relatively quickly at speeds of approximately 3000 r.p.m. The axis 68 of rotation of each refiner blade is orthogonal to the axis of rotation of the slowly rotating paddles 65a, which rotate at tip speeds in the range 4 to 6 m/s, preferably 5-5.5 m/s. The quickly rotating refiner mixers 67 are primarily intended to chop up the larger particles of shredded pulp after the latter have swollen in the amine oxide solution. The slowly rotating paddles are intended to mix the introduced components together to facilitate dispersion of the cellulose in the amine oxide solution. The combined actions of the slowly rotating paddles 65a and the quickly rotating refiner mixers 67, produces a homogeneously mixed mixture of the cellulosic material dispersed in the amine oxide and water. The items 65c, 67b and 83e shown in Figure 4 represent part of an electronic computer control system for automatically controlling the entire process and, in particular, the motor 65b, the motors 67a and a mass flow meter upstream of valve 83c, respectively. The external casing of each premixer, which provides the walls of the mixing chamber, has heating jackets 69 around which hot water, typically at a temperature of about 180°F (82°), e.g. 176°F (80°C), is circulated to retain the contents of each mixing chamber at an elevated temperature of about 180°F (82°C), e.g. 176°F (80°C). Hot water is supplied via supply pipe 69a and is returned for re-heating via return pipe 69b. Each mixing operation typically takes about 21 minutes to perform. The amine oxide solution is initially loaded into the premixer in about 5 minutes and the pulp and added propyl gallate are subsequently loaded over a period of about 10 minutes. Mixing then proceeds for at least four minutes, typically for about 6 minutes, at an elevated temperature of about 180 β F (82°C), e.g. 176°F (80°C), in which time a high quality mixture is obtained in which the cellulosic material is broken down into discrete individual fibers which are substantially uniformly dispersed in the tertiary amine oxide. The result is a premix having a relatively high cellulose content of about 13%. The premix can subsequently be converted under the action of heat and pressure into a viscous dope in which the cellulose is dissolved in the amine oxide solution, the dope so produced being suitable for subsequently producing cellulosic products. A particularly suitable mixer has been found to be the RT3000 Model Mixer manufactured by Winkworth Machinery Limited at Swallowfield, Near Reading, Berkshire, United Kingdom. The premixers 7a and 7b have valved bottom outlets 82a and 82b which are connected, respectively, to the inlets 83a and 83b of vertical storage hoppers 84 and 85. The hoppers 84 and 85 have outlets 86 and 87, respectively, which are connected to inlet sides of reciprocating piston pumps 88 and 89, respectively. The pumps 88 and 89 have outlet pipes 90 and 91, respectively, connected to a dope making stage (not shown). Depending on which batch is being processed, the mixture is either passed from premixer 7a, via the storage hopper 84 to the piston pump 88 for conveyance via outlet pipe 90 to the dope making stage or is passed from premixer 7b, via the storage hopper 85 to the piston pump 89 for conveyance via outlet pipe 91 to the dope making stage. The storage hoppers 84 and 85 serve to maintain the mixture formed in the premixers 7a and 7b, respectively, in a mixed homogeneous condition of the correct consistency and viscosity. Since the storage hoppers 84 and 85 are identical and the reciprocating piston pumps 88 and 89 are identical only storage hopper 84 and piston pump 88 will be described in detail hereafter. The storage hopper 84 (shown schematically in Figure 5) is arranged vertically and has a circular cylindrical upper portion 84a and a frusto-conical lower portion 84b. Heating pipes 84c are arranged on the outside of the portions 84a and 84b for passing hot water around the walls of the hopper to maintain the contents of the hopper at an elevated temperature of about 180°F (82°C), e.g. 176°F (80°C). Hot water is supplied via inlets 84h and 84i and is returned via outlets 84j and 84k. Inside the storage hopper 84, a vertical, axially disposed shaft 84d carrying axially spaced apart radial arms 84e is rotatable at a relatively slow speed of from 2-10 r.p.m., e.g. 8 r.p.m.. The shaft 84d is supported by an upper bearing (not shown), a lower bearing 84g and an intermediate bearing carried by radial arms 84p. Axially adjacent pairs of the arms 84e carry a common stirrer 84f, with four such stirrers 84f being shown in Figure 4. These stirrers 84f are positioned at the radially outer extremities of the arms 84e and in use sweep out stirring paths adjacent the walls of the hopper 84. In use the stirrers 84f act to stir premix contained in both the upper portion 84a and the lower portion 84b of the storage hopper 84. In Figure 5 only half the numbers of arms 84e and stirrers 8 f are shown since corresponding arms and stirrers (not shown) extend on the right hand side of the hopper 84, each arm on the right hand side being diametrically in line with its corresponding arm 84e. The arms 84e carrying the upper stirrer 84f in the upper portion 84a and aligned with (i.e. are in the same axial plane) as the arms 84e carrying the upper stirrer 84f in the lower portion 84b. The arms 84e carrying the lower stirrer 84f in the upper portion 84a and the arms 84e carrying the lower stirrer 84f in the lower portion 84b are also aligned in a common plane which is offset, e.g. 90°, from the axial plane containing the other radial arms 84e. It will be appreciated that Figure 5 is only schematic since the offset radial arms are all shown. The premix passed into the storage hopper 84 can be kept in a viscous usable condition at the correct elevated temperature for a desired period of time, e.g. up to several hours. The relatively slowly rotating stirrers 84f keep the cellulose dispersed in the amine oxide solution so that the mixture remains in a homogeneous condition. The premix. can thus be kept in a usable condition for a period of time before being transported to the dope forming stage and serves to provide a useful degree of control in the production process. Thus the storage hopper 84 provides a break in the process and is able to absorb any discontinuities upstream, e.g. caused by having to stop the process for system failures or the like, without the need to discard the already mixed premix. The reciprocating piston pump 88 is a dual piston, hydraulically actuated so-called "concrete pump". A particularly suitable concrete pump is the Schwing Type KSP 17 HD EL pump manufactured by Schwing GmbH. Such a concrete pump 88 is found to be particularly suitable for conveying the premix to the dope forming stage without the premix losing its homogeneity. In use, the premix is delivered, on opening of a valve 95, through an outlet of the hopper 84 into an inlet 96 (see Figures 6 and 7) of the pump 88. On the suction stroke of one of the pistons of the dual piston pump, the premix is drawn through the outlet of the hopper into one of the two cylinders 97, 98 of the pump 88. On the subsequent forward discharge stroke of the piston, the premix previously drawn into the cylinder is pushed forward through a transfer tube 99 for conveyance through the outlet pipe 90. The transfer pipe 99 is mounted on pivot shaft 100 and, on actuation of an hydraulic ram 105, is pivotally movable between a position shown in full lines in Figure 7 in which the cylinder 98 is connected to the pipe 90 and a position shown in dashed lines in Figure 7 in which the cylinder 97 is connected to the pipe 90. Alternatively flow from the alternate cylinders can be controlled by poppet valves. In Figure 7, opening 101 (shown in chain lines) is the inlet of the outlet pipe 90 and openings 102 and 103 are at the ends of the cylinders 97 and 98, respectively. The operation of the transfer pipe 100 and of the rest of the pump 88 is described in more detail in Schwing US Patent No. 4,373,875 the entire contents of which are incorporated herein by way of reference. The reciprocating piston pump 88 is found to be robust in use and provides a positive pumping action for conveying the cellulosic premix. The relatively slowing reciprocating pistons do not "squeeze out" and separate the amine oxide from the cellulose to any significant degree and do not break down the cellulose. This is primarily because a large proportion of the kinetic energy of the moving pistons is used to move the premix. Moreover the pump acts as a metering pump. Since the volume of each cylinder is known and since each cylinder is filled with premix on a suction stroke, the amount of premix discharged on each discharge stroke can be accurately determined. Thus the amount of premix being conveyed over a period of time can be accurately controlled by controlling the speed of the reciprocating pistons. The pump is relatively reliable in use, does not cause the cellulose to be separated out from the amine oxide and accurately meters the premix. The premix contains approximately 13% by weight of cellulose and the reciprocating piston pump is able to pump the premix reliably and effectively. The premix from the pumps 88, 89 is conveyed via hot water traced pipes 90,91 to a dope forming stage, the dope so formed subsequently being shaped and regenerated into a cellulosic product, such as a fiber, filament, rod, tubing, plate or film. The pipes 90 and 91 are provided with valves 92a and 92b, respectively, and reciculating pipes 93a and 93b are connected upstream of the valves 92a and 92b for connecting the outlets of the pumps 88 and 90 to inlets of the storage hoppers 7a and 7b. The recirculating pipes 93a and 93b incorporate valves 94a and 94b, respectively. By closing the valves 92a and 92b and opening the valves 94a, 94b and 95, premix can be pumped around closed circuits including the storage hoppers 7a and 7b without having to be pumped to the dope forming station. Thus if a blockage occurs in the pipes 90, 91 downstream of the valves 92a, 92b, these valves can be closed and the mixture can be recirculated back to the storage hoppers. In the apparatus described much of the piping is lagged. In particular the hot water supply lines 83d and 96a and the supply lines (not shown) connected to hopper inlets 84h and 84i are lagged as are the lines connecting premixer outlets 82a and 82b to the storage hopper inlets 83a and 83b, respectively. The outlet pipes 90 and 91 are also lagged. Although not shown and described in detail herein, the steps of controlling the feeding of web from the paper rolls to the shredding apparatus, of supplying the shredded pulp to the premixers including the step of recovering fine particles filtered from the shredded pulp, of adding desired quantities of premix constituents to the premixers, of mixing the premix constituents in the premixers, of stirring the formed premix in the storage hoppers and of pumping the premix to a dope forming stage is preferably automatically controlled under computer control. INDUSTRIAL APPLICABILITY The invention finds application in the textile industry for the production of cellulosic products.

Claims: CLAIMS 1. A method of conveying by means of pumping apparatus a mixture of cellulose and at least one liquid, the mixture consisting of at least 8% by weight of cellulose, characterised in that the pumping apparatus comprises a reciprocating piston pump (88,89). 2. A method according to claim 1, characterised in that said mixture consists of up to 20% by weight of cellulose. 3. A method according to claim 1 or 2, characterised in that the said pump (88,89) comprises a plural cylinder concrete pump. 4. A method according to any of the preceding claims, characterised in that the said pump (88,89) comprises a two cylinder concrete pump. 5. A method according to any of the preceding claims, characterised in that the pump (88,89) is hydraulically actuated. 6. A method according to any of the preceding claims, characterised in that the said mixture comprises cellulose, amine oxide and water. 7. A method according to any of the preceding claims, characterised in that the said mixture comprises approximately 13 parts by weight of cellulose and 87 parts by weight of amine oxide and water. 8. A method according to any of the preceding claims, characterised in that the said mixture comprises approximately 13 parts by weight of cellulose, 68 parts by weight of amine oxide and 19 parts by weight of water. 9. A system for preparing and conveying a cellulose containing liquid mixture characterised in that the system comprises a premixer (7a,7b) having inlets (80,81,83) for the introduction of amine oxide, water and cellulosic material, stirring means (65,65a) for stirring amine oxide, water and cellulosic material introduced into the premixer to form a mixture and outlet means (82a,82b); a storage hopper (84,85) having inlet means (83a, 83b) connected to the outlet means (82a,82b) of the premixer (7a,7b) for enabling the mixture to be introduced into the storage hopper and outlet means (86,87); and a reciprocating piston pump (88,89) connected to the outlet means (86,87) of the storage hopper so that the mixture can be introduced from the storage hopper (84,85) into the piston pump (88,89) for onward conveyance via ducting (90,91) to a further processing station. 10. A system according to claim 9, characterised in that the said reciprocating piston pump (88,89) comprises a concrete pump. 11. A system according to claim 9, characterised in that the reciprocating piston pump (88,89) has plural cylinders and comprises a concrete pump.

Inventors: GRAY GARY EDWARD GEORGE, JACK IAIN RICHARD, GRAY, GARY, EDWARD, GEORGE, JACK, IAIN, RICHARD
Applicants: COURTAULDS FIBRES HOLDINGS LTD, COURTAULDS FIBRES (HOLDINGS) LIMITED
Application year: 1994
Main classification: D01F2
IPC codes: B65G53, D01D1, D01F2